EP2591071B1 - Régénération ascendante de catalyseur fcc pour craquage à plusieurs étages - Google Patents

Régénération ascendante de catalyseur fcc pour craquage à plusieurs étages Download PDF

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Publication number
EP2591071B1
EP2591071B1 EP11741289.0A EP11741289A EP2591071B1 EP 2591071 B1 EP2591071 B1 EP 2591071B1 EP 11741289 A EP11741289 A EP 11741289A EP 2591071 B1 EP2591071 B1 EP 2591071B1
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EP
European Patent Office
Prior art keywords
catalyst
regenerator
upflow
spent catalyst
diameter zone
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EP11741289.0A
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German (de)
English (en)
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EP2591071A1 (fr
Inventor
S. Mukthiyar
P. R. Pradeep
Debasis Bhattacharyya
V. K. Satheesh
G. Saidulu
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Indian Oil Corp Ltd
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Indian Oil Corp Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0025—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by an ascending fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/12—Treating with free oxygen-containing gas
    • B01J38/30—Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • B01J8/30—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other the edge of a lower bed projecting beyond the edge of the superjacent bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C10G11/182—Regeneration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects
    • C10G2300/708—Coking aspect, coke content and composition of deposits

Definitions

  • the present invention relates to the area of Fluidized Catalytic Cracking (FCC) of heavy hydrocarbons into lighter fractions with a fluidized stream of catalyst.
  • FCC Fluidized Catalytic Cracking
  • this invention relates to the improved process of regeneration of spent catalyst comprising varying level of coke from multiple fluidized bed catalytic cracking reactors resulting in reduced hydrothermal and metal deactivation of catalyst and also an apparatus thereof.
  • the present invention provides an improved process for regeneration of FCC spent catalysts of varying coke content from multiple fluidized bed catalytic cracking reactors employing upflow regenerator of multiple diameter zones.
  • the spent catalyst containing the highest coke content is fed at the bottom of the upflow regenerator and the spent catalysts containing lesser coke content are fed at higher elevations than the feeding point of highest coke content spent catalyst.
  • the elevation of feeding point of each spent catalyst to the upflow regenerator is so designed such that the residence time required for the spent catalyst to burn the coke to the desired level.
  • the regenerator system may be operated in more than one fluidization regime without the use of additional structural elements like placing an internal vessel, vertical partition or a baffle.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (7)

  1. Procédé de régénération améliorée de catalyseurs usés de craquage catalytique fluide (FCC) à teneur variable en coke provenant de multiples réacteurs FCC en employant un régénérateur à courant ascendant ayant au moins une première zone de diamètre et une deuxième zone de diamètre comprenant :
    - l'introduction du premier catalyseur usé provenant d'un premier réacteur FCC par le bas de la première zone de diamètre du régénérateur à courant ascendant, et
    - l'introduction du deuxième catalyseur usé provenant d'un deuxième réacteur FCC dans la deuxième zone de diamètre, à une hauteur plus élevée que le point d'introduction du premier catalyseur usé dans un régénérateur à courant ascendant,
    - la séparation d'un catalyseur régénéré provenant de la première zone de diamètre et de la deuxième zone de diamètre du régénérateur à courant ascendant à partir de gaz de combustion dans un système de séparation et de cyclones fournis au sommet du régénérateur à courant ascendant,
    dans lequel la teneur en coke du premier catalyseur usé est au moins de 0,1 % en poids supérieure à la teneur en coke du deuxième catalyseur usé et le temps de présence des premier et deuxième catalyseurs usés dans le régénérateur à courant ascendant est déterminé sur la base de la teneur en coke respective, et dans lequel une désactivation hydrothermique et métallique du premier catalyseur usé et du deuxième catalyseur usé est minimisée ;
    dans lequel un temps de présence d'un catalyseur est situé dans la plage allant de 5 à 30 secondes dans la première zone de diamètre tandis que le temps de présence d'un catalyseur dans la deuxième zone de diamètre est situé dans la plage allant de 10 à 30 secondes,
    dans lequel un diamètre de la première zone de diamètre est inférieur au diamètre de la deuxième zone de diamètre ; et dans lequel une hauteur de la première zone de diamètre est plus basse qu'une hauteur de la deuxième zone de diamètre.
  2. Procédé selon la revendication 1, dans lequel la teneur en coke du premier catalyseur usé varie dans la plage allant de 0,4 à 3 % en poids.
  3. Procédé selon la revendication 1, dans lequel la teneur en coke du deuxième catalyseur usé varie dans la plage allant de 0,3 à 2,9 % en poids.
  4. Procédé selon la revendication 1, dans lequel la vitesse superficielle d'un gaz dans toutes les zones du régénérateur à courant ascendant est maintenue au-dessus de 2 m/sec.
  5. Procédé selon la revendication 1, dans lequel le régénérateur à courant ascendant fonctionne avec plus de deux zones de diamètre correspondant au nombre de points d'introduction du catalyseur usé, un catalyseur présentant une teneur en coke la plus élevée entrant par le bas de la zone de diamètre la plus petite située dans la partie la plus basse du régénérateur et le catalyseur présentant la teneur en coke la plus basse entrant par le bas de la zone de diamètre la plus grande située dans la partie la plus haute du régénérateur.
  6. Procédé selon la revendication 1, dans lequel des gaz contenant de l'air ou de l'oxygène sont injectés à différentes hauteurs en tant que milieux réactionnels et d'élévation le long de la longueur du régénérateur à courant ascendant.
  7. Procédé selon la revendication 1, dans lequel les réacteurs FCC incluent des réacteurs à courant ascendant, à courant descendant, à courant incliné, à lit agité ainsi qu'à lit dense en n'importe quel nombre sous une sévérité de fonctionnement variable utilisant des catalyseurs et additifs de craquage.
EP11741289.0A 2010-07-08 2011-07-04 Régénération ascendante de catalyseur fcc pour craquage à plusieurs étages Active EP2591071B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IN747KO2010 2010-07-08
PCT/IN2011/000441 WO2012004805A1 (fr) 2010-07-08 2011-07-04 Régénération ascendante de catalyseur fcc pour craquage à plusieurs étages

Publications (2)

Publication Number Publication Date
EP2591071A1 EP2591071A1 (fr) 2013-05-15
EP2591071B1 true EP2591071B1 (fr) 2018-12-12

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US (1) US20130172173A1 (fr)
EP (1) EP2591071B1 (fr)
TR (1) TR201903230T4 (fr)
WO (1) WO2012004805A1 (fr)

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CN103509596B (zh) * 2013-09-29 2015-08-26 中国石油大学(北京) 一种加工劣质重油的方法
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CN105566023B (zh) * 2014-10-14 2017-11-21 中国石油化工股份有限公司 高效混合的甲醇制烯烃反应‑再生装置及其反应方法
BR112018072147A2 (pt) * 2016-04-29 2019-02-12 Basf Corporation projeto de unidade de desativação de metal cíclica novo para a desativação de catalisador de fcc
US10781377B2 (en) * 2017-11-30 2020-09-22 Uop Llc Process and apparatus for cracking hydrocarbons to lighter hydrocarbons
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Also Published As

Publication number Publication date
TR201903230T4 (tr) 2019-03-21
EP2591071A1 (fr) 2013-05-15
WO2012004805A1 (fr) 2012-01-12
US20130172173A1 (en) 2013-07-04

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